US3674429A - Adsorption process for water and nitrogen oxides - Google Patents
Adsorption process for water and nitrogen oxides Download PDFInfo
- Publication number
- US3674429A US3674429A US104262A US3674429DA US3674429A US 3674429 A US3674429 A US 3674429A US 104262 A US104262 A US 104262A US 3674429D A US3674429D A US 3674429DA US 3674429 A US3674429 A US 3674429A
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- bed
- silica gel
- water
- molecular sieve
- heat sink
- Prior art date
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/92—Chemical or biological purification of waste gases of engine exhaust gases
- B01D53/94—Chemical or biological purification of waste gases of engine exhaust gases by catalytic processes
- B01D53/9481—Catalyst preceded by an adsorption device without catalytic function for temporary storage of contaminants, e.g. during cold start
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/52—Hydrogen sulfide
- B01D53/523—Mixtures of hydrogen sulfide and sulfur oxides
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/52—Hydrogen sulfide
- B01D53/526—Mixtures of hydrogen sulfide and carbon dioxide
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B21/00—Nitrogen; Compounds thereof
- C01B21/20—Nitrogen oxides; Oxyacids of nitrogen; Salts thereof
- C01B21/36—Nitrogen dioxide (NO2, N2O4)
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G5/00—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas
- C10G5/04—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas with liquid absorbents
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
- C10K1/16—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with non-aqueous liquids
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
- B01D2253/106—Silica or silicates
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
- B01D2253/106—Silica or silicates
- B01D2253/108—Zeolites
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/10—Single element gases other than halogens
- B01D2257/102—Nitrogen
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/10—Single element gases other than halogens
- B01D2257/104—Oxygen
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/40—Nitrogen compounds
- B01D2257/404—Nitrogen oxides other than dinitrogen oxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/401—Further details for adsorption processes and devices using a single bed
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/414—Further details for adsorption processes and devices using different types of adsorbents
- B01D2259/4141—Further details for adsorption processes and devices using different types of adsorbents within a single bed
- B01D2259/4145—Further details for adsorption processes and devices using different types of adsorbents within a single bed arranged in series
- B01D2259/4146—Contiguous multilayered adsorbents
Definitions
- the heat sink serves to prevent premature desorption of water from the silica gel bed and the contact of liquid water with desorbed N
- the present invention relates, in general, to the removal of nitrogen oxides from gas streams containing same in addition to water vapor, and more particularly, to an improved process for such removal using a dual adsorbent system comprising silica gel and a Zeolitic molecular sieve, the two adsorbent masses being separated by an inert solid heat sink.
- nitric acid is currently produced on a commercial scale by the catalyzed oxidation of ammonia and the subsequent reaction of N0 or N 0 with water.
- the initial reaction between oxygen and ammonia produces a mixture of water and nitrogen oxides principally as nitric oxide, i.e., NO.
- a secondary oxidation step further converts the nitric oxide to nitrogen dioxide, N0 and/or the dimer form of N0 namely dinitrogen tetraoxide, N 0
- the absorption of N0 and/or N 0 in water spontaneously produces nitric acid in accordance with one or both of the equations:
- the waste or tail gas from the aqueous absorbed contains normally about 0.15 to 0.3 mole percent unabsorbed oxides of nitrogen (commonly expressed as NO,,), principally NO and N0
- NO unabsorbed oxides of nitrogen
- the tail gas from which the NO values are to be recovered contains water vapor. There are present in the gas stream, therefore, all of the necessary reagents for forming nitric acid, and the surface of most solids appears to facilitate the contact of these reagents.
- a solid sorbent, to be useful in this application must, accordingly, be able to withstand the corrosiveness of aqueous nitric acid of any and all concentrations. There are, moreover, only relatively few adsorbents which are practical possibilities from the standpoint of availability and cost.
- this process comprises contacting a gas mixture comprising water vapor, nitrogen, and at least one of the gases NO and N0 said gas stream also containing oxygen when N0 is absent therefrom, with an adsorbent bed of activated (dehydrated) silica gel sufiicient to adsorb the water vapor therefrom, then contacting the gas mixture constituents unadsorbed by said silica gel with a zeolite, preferably of the cage type, having a pore size large enough to admit N0 i.e., at least about 4 angstroms whereby NO is catalytically oxidized to N0 and N0 is adsorbed in said zeolite, and thereafter desorbing the N0 from the zeolite adsorbent, and the water from the silica gel.
- a zeolite preferably of the cage type, having a pore size large enough to admit N0 i.e., at least about 4 angstroms whereby NO is catalytically oxidized to N0 and
- the incoming gas stream is dried by contact with the silica gel bed which does not adsorb N0 appreciably at the temperatures involved, and the N0 is thereafter adsorbed on the molecular sieve bed in the absence of moisture.
- This procedure prevents the formation of nitric acic in the molecular sieve bed with resultant degradation of that adsorbent.
- Desorption of the adsorption system is accomplished by passing a hot dry inert stripping purge gas stream such as air countercurrently through the dual bed system.
- the general object of the present invention to provide an improvement in the aforesaid process which avoids, or greatly reduces, the formation of corrosive aqueous nitric acid during adsorption system regeneration, and, hence, the need for the more expensive and corrosion-resistant apparatus.
- the process for recovering nitrogen oxides which comprises the steps of providing a gas stream comprising water vapor, nitrogen and at least one of the gases NO and N0 said gas stream also containing oxygen when N0 is absent therefrom, contacting said gas stream with an adsorbent silica gel in relative proportions and for sufiicient time to remove substantially all of the water vapor therefrom, and thereafter contacting the resulting dehydrated gas stream with an activated crystalline zeolitic molecular sieve adsorbent whereby at least some of any NO present is oxidized to N0 and N0 is adsorbed thereon, the aforesaid objective is accomplished by the improvement which comprises providing a solid heat sink and passing the eflluent purge gas from the molecular sieve bed therethrough prior to passing said stream through the silica gel bed at least during the period when the temperature of the effiuent gas from the molecular sieve bed is essentially as high as the purge gas entering the inlet end of the molecular sieve bed, the heat
- the present invention is advantageously exemplified, illustrated and its elements amplified by the following description in conjunction with the drawing which is a schematic flow sheet using a single compound adsorbent bed.
- the feed stream to be treated is considered for purposes of this illustration to be a Waste gas stream from a nitric acid plant containing NO, N0 N 0 and saturated with respect to water vapor.
- gas mixtures of primary interest in the present invention are tail gases or stack gases from nitric acid plants
- the process is equally suitable for removing NO and/ or N from any gas stream which contains same in combination with water vapor and any other gases which are not destructive of the adsorbent materials, especially the zeolitic molecular sieves. Since NO is not strongly adsorbed by zeolites, stoichiometric quantities of oxygen must be present with respect to the quantity of NO which is to be removed.
- gaseous substances which can be a part of the gas mixture being treated are argon, helium, neon and carbon dioxide.
- a representative tail gas stream from an ammonia oxidation type HNO process contains in parts by volume,
- the silica gel employed as the desiccant in the process can be any of the numerous commercially-available adsorbent grade materials such as are obtained by the suitable coagulation of hydrated silica obtained by destabilizing an aqueous silicate solution.
- the silica gel is, of course, activated or to a substantial degree dehydrated at the start-up of the NO recovery process.
- any zeolitic molecular sieve both natural and synthetic, can be used to remove the NO and N0 from the gas stream, provided the zeolite has a pore size suificient to admit N0
- zeolite K-G disclosed in U.S. Pat. 3,056,654
- zeolite W disclosed in U.S. Pat. 3,012,853
- zeolite S disclosed in U.S. Pat. 3,054,657
- zeolite T disclosed in U.S. Pat.
- zeolite X disclosed in U.S. Pat. 2,882,244, zeolite A disclosed in U.S. Pat. 2,882,243, zeolite Y disclosed in U.S. Pat. 3,130,007, and zeolite L disclosed in U.S. Pat. 3,216,789.
- Suitable naturally-occurring zeolitic molecular sieves include chabasite, erionite, gmelinite, mordenite, and faujasite. The synthetic forms of mordenite are also suitable. It is to be understood that no known zeolitic molecular sieve per se adsorbs nitric oxide to a significant degree.
- zeolitic molecular sieves do, however, have at least some ability to catalyze the oxidation of NO to N0 in the presence of oxygen. Further, zeolite adsorbed N0 appears to be able to combine with NO to form N 0 which is retained as an adsorbate or further oxidized to N 0 The precise mechanism of adsorption of the NO values is not a critical matter to the present process.
- the feed stream is introduced into the system through line 50 at a temperature of about 90 F. under a pressure of about 90 p.s.i. Because considerable water can be removed from the water saturated feed stream by lowering its temperature, line 50 conducts the feed stream to cooler-condenser 52, wherein the temperature is reduced to about 60 F., and the water condensed from the gas stream is removed through line 54.
- the partially dehydrated feed gas thus produced is passed through line 56 and valve 58 to dual adsorbent bed 60 containing in the first section thereof to be contacted by the incoming gas stream, silica gel.
- the second section of the adsorbent bed contains the' inert solid heat sink material, and the third section contains the zeolitic molecular sieve.
- the adsorptive capacity of the silica gel for water increases with increasing pressure within the pressure range herein contemplated.
- the temperature of the gas entering the desiccant bed on the adsorption stroke will be between about 60 F. and about F and at a pressure of about p.s.i.g., but temperatures of from 40 F. to F. and pressures of from about 1 atmosphere to 30 atmospheres are suitably employed.
- Substantially all of the remaining water is removed as the gas stream passes through the silica gel bed.
- the dehydrated gas then passes through the heat sink section. If, due to the heat sink portion of the bed happens to be cooler than the gas stream entering from the silica gel portion, the heat sink portion will exhibit a recooperator type behavior.
- Such behavior i.e., the Withholding of the heat front to some extent from the molecular sieve bed, is beneficial in that the capacity of the molecular sieve for adsorbing N0 increases, within limits, with decreasing temperat-ures.
- N 0 initially present in the feed stream and NO oxidized to N0 is adsorbed in the molecular sieve portion of the bed.
- the efiluent from bed 60 principally nitrogen and oxygen, is directed partially or wholly through valve 62 and out line 64 to power recovery, or through heater 66 and valve 68, or through line 70 and valve 68 (thereby by-passing the heater 66) through adsorbent bed 72.
- This latter adsorbent bed advantageously contains a molecular sieve having a large capacity for H 0 such as zeolite 4A, i.e., the sodium form of zeolite A.
- the dry efiluent gas from bed 60 serves to desorb any water vapor from bed 72.
- the heater 66 is advantageously employed.
- the regeneration of the compound bed 60 is accomplished by countercurrent strip purging using a hot dry inert purge gas such as air or nitrogen.
- a hot dry inert purge gas such as air or nitrogen.
- the purge gas stream ordinarily at ambient temperature, is fed through line 74 to bed 72 to insure that the purge gas is substantially fully dehydrated and then passed through valve 68 to heater 66 where its temperature is, if necessary, raised to a temperature of between 250 F. and 750 F.
- the hot purge gas leaving heater 66 is directed through valve 62 to the molecular sieve portion of compound bed 60.
- the incoming hot purge gas establishes an advancing heat front in the bed in the molecular sieve section, and carries desorbed N0 toward the silica gel end of the bed.
- the heat front eventually leaves the molecular sieve section and is re-established in the heat sink section before the bulk of the N0 has been purged from the molecular sieve.
- the heat sink material delaying the establishment of the hot purge heat front in the silica gel section, permits at least 50% of the N0 initially adsorbed in the molecular sieve section to have passed out of the silica gel section before the hot purge begins to desorb water therefrom.
- the kind of material used in the heat sink and the size of the heat sink will vary depending on several variable factors. These factors include the size and configuration of the various bed sections, the particular molecular sieve employed and the size and composition of the agglomerated zeolite forms, the degree to which the adsorptive capacity of either the silica gel or the molecular sieve sections of the bed are loaded during the adsorption stroke, the temperature of the purge gas, and numerous others which are routinely fixed in accordance with good engineering practice in view of the particular feed stream being treated.
- the materials which comprise the heat sink can be any material which will not to any significant degree alter the gas stream passing over it, either by reaction with the components or by adsorbing nitrogen oxide.
- Shaped forms such as pellets, bricks or beads or irregular forms such as are formed by crushing larger bodies of glass, quartz, metal, mineral rocks, beach pebbles and the like. Materials of high heat capacity and good thermal conductivity are to be preferred in order to limit the size of the heat sink section to reasonable proportions.
- a cool purge gas stream is employed to return the bed 60 to adsorption stroke temperature.
- this cool-down is accomplished by continuing the strip purge operation, but by passing heater 66 using valves 62 and 68 and line 70.
- the effluent from condenser 52 can be fed through valve 84, line 78, heater 80 and line 82 before entering bed 60.
- the heater is used to raise the temperature of the gas stream about 5 F. to 35 F. in order to at least revaporize the droplets, and preferably also to insure that the gas stream contacting the silica gel is less than saturated with respect to H O.
- the process for recovering nitrogen oxides which comprises the steps of providing a gas stream comprising water vapor, nitrogen and at least one of the gases NO and N0 said gas stream also containing oxygen when N0 is absent therefrom, contacting said gas stream with an adsorbent silica gel in relative proportions and for sufiicient time to remove substantially all of the water vapor therefrom, and thereafter contacting the resulting dehydrated gas stream with an activated crystalline zeolitic molecular sieve adsorbent whereby at least some of any NO present is oxidized to N0 and N0 is adsorbed thereon, the improvement which comprises providing a solid heat sink and passing the effluent purge gas from the molecular sieve bed therethrough prior to passing said stream through the silica gel bed at least during the period when the temperature of the effluent gas from the molecular sieve bed is at least as high as the purge gas entering the inlet end of the molecular sieve bed, the heat sink having sufiicient heat capacity to prevent the heat front leaving
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Analytical Chemistry (AREA)
- Organic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Environmental & Geological Engineering (AREA)
- Combustion & Propulsion (AREA)
- Materials Engineering (AREA)
- Inorganic Chemistry (AREA)
- Solid-Sorbent Or Filter-Aiding Compositions (AREA)
- Separation Of Gases By Adsorption (AREA)
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US10426271A | 1971-01-06 | 1971-01-06 |
Publications (1)
Publication Number | Publication Date |
---|---|
US3674429A true US3674429A (en) | 1972-07-04 |
Family
ID=22299503
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US104262A Expired - Lifetime US3674429A (en) | 1971-01-06 | 1971-01-06 | Adsorption process for water and nitrogen oxides |
Country Status (11)
Country | Link |
---|---|
US (1) | US3674429A (de) |
JP (1) | JPS5123959B1 (de) |
AU (1) | AU458612B2 (de) |
BE (1) | BE777726A (de) |
CA (1) | CA961239A (de) |
DE (1) | DE2200210C3 (de) |
FR (1) | FR2121599B1 (de) |
GB (1) | GB1357701A (de) |
IT (1) | IT948802B (de) |
NL (1) | NL170838C (de) |
SE (1) | SE382803B (de) |
Cited By (26)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3719025A (en) * | 1970-11-11 | 1973-03-06 | Bayer Ag | Resolving gas mixtures |
US4100421A (en) * | 1975-12-19 | 1978-07-11 | Mitsubishi Denki Kabushiki Kaisha | Ozone-generating apparatus |
US4146372A (en) * | 1976-03-29 | 1979-03-27 | Mittex Aktiengesellschaft | Process and system for recovering water from the atmosphere |
US4220632A (en) * | 1974-09-10 | 1980-09-02 | The United States Of America As Represented By The United States Department Of Energy | Reduction of nitrogen oxides with catalytic acid resistant aluminosilicate molecular sieves and ammonia |
US4336159A (en) * | 1979-09-12 | 1982-06-22 | Ceag Verfahrenstechnik Gmbh | Method and arrangement for the thermal regeneration of charged adsorption materials |
US4367204A (en) * | 1979-05-04 | 1983-01-04 | Budapesti Muszaki Egyetem | Process for the recirculation of nitrogen oxides |
US4398927A (en) * | 1980-07-30 | 1983-08-16 | Exxon Research And Engineering Co. | Cyclic adsorption process |
US4472178A (en) * | 1983-07-05 | 1984-09-18 | Air Products And Chemicals, Inc. | Adsorptive process for the removal of carbon dioxide from a gas |
US4473381A (en) * | 1982-01-19 | 1984-09-25 | CEAG Verfahrungstechnik GmbH | Method for recovering a substantially dehydrated desorbate as well as apparatus for carrying out the method |
US4533365A (en) * | 1982-07-17 | 1985-08-06 | Kernforschungsanlage Julich Gesellschaft Mit Beschrankter Haftung | Process for the separation and recycling of NOx gas constituents through adsorption and desorption on a molecular sieve |
US4586940A (en) * | 1983-09-29 | 1986-05-06 | Simmering-Graz-Pauker Aktiengesellschaft | Process and apparatus for a recovery of heat comprising a heat-recovering absorption of water vapor from gases |
US4631074A (en) * | 1981-12-15 | 1986-12-23 | Didier-Werke Ag | Method and apparatus for reducing the temperature of air |
US4698073A (en) * | 1983-10-06 | 1987-10-06 | Linde Aktiengesellschaft | Process for regeneration of adsorbers |
US5080876A (en) * | 1989-04-21 | 1992-01-14 | Mitsubishi Jukogyo Kabushiki Kaisha | Self-reactivating type denitrating method |
US5169413A (en) * | 1991-10-07 | 1992-12-08 | Praxair Technology Inc. | Low temperature pressure swing adsorption with refrigeration |
US5264198A (en) * | 1991-03-29 | 1993-11-23 | Mainstream Engineering Corporation | Method for production of spacecraft-grade N2 O4 |
US5417950A (en) * | 1994-07-07 | 1995-05-23 | The Boc Group, Inc. | Process for the purification of nitric oxide |
US5580369A (en) * | 1995-01-30 | 1996-12-03 | Laroche Industries, Inc. | Adsorption air conditioning system |
US5614000A (en) * | 1995-10-04 | 1997-03-25 | Air Products And Chemicals, Inc. | Purification of gases using solid adsorbents |
US5670125A (en) * | 1993-09-30 | 1997-09-23 | The Boc Group, Inc. | Process for the purification of nitric oxide |
US5919286A (en) * | 1997-03-06 | 1999-07-06 | Air Products And Chemicals, Inc. | PSA process for removel of nitrogen oxides from gas |
US6106593A (en) * | 1998-10-08 | 2000-08-22 | Air Products And Chemicals, Inc. | Purification of air |
US6231824B1 (en) | 1999-08-10 | 2001-05-15 | The Boc Group, Inc. | Removal of nitric oxide from gas streams |
US6576044B1 (en) | 1999-02-25 | 2003-06-10 | The Boc Group, Inc. | Process for the purification of nitric oxide |
WO2010033916A1 (en) * | 2008-09-22 | 2010-03-25 | Geno Llc | Conversion of nitrogen dioxide (no2) to nitric oxide (no) |
EP4157486A4 (de) * | 2020-05-26 | 2024-07-10 | Nicholas Stuckert | Kombinierte wärmeenergiespeicherung und schadstoffentfernung |
Families Citing this family (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB1460595A (en) * | 1974-02-22 | 1977-01-06 | Cjb Developments Ltd | Process for the removal of carbon dioxide from gases |
JPS60173592U (ja) * | 1984-04-27 | 1985-11-16 | 三和テッキ株式会社 | 電界検知型ブ−ム |
-
1971
- 1971-01-06 US US104262A patent/US3674429A/en not_active Expired - Lifetime
- 1971-12-16 CA CA130,246A patent/CA961239A/en not_active Expired
-
1972
- 1972-01-04 SE SE7200074A patent/SE382803B/xx unknown
- 1972-01-04 DE DE2200210A patent/DE2200210C3/de not_active Expired
- 1972-01-05 GB GB41372A patent/GB1357701A/en not_active Expired
- 1972-01-05 NL NLAANVRAGE7200138,A patent/NL170838C/xx not_active IP Right Cessation
- 1972-01-05 IT IT67034/72A patent/IT948802B/it active
- 1972-01-05 BE BE777726A patent/BE777726A/xx not_active IP Right Cessation
- 1972-01-05 FR FR7200251A patent/FR2121599B1/fr not_active Expired
- 1972-01-05 AU AU37594/72A patent/AU458612B2/en not_active Expired
- 1972-01-05 JP JP47000038A patent/JPS5123959B1/ja active Pending
Cited By (34)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3719025A (en) * | 1970-11-11 | 1973-03-06 | Bayer Ag | Resolving gas mixtures |
US4220632A (en) * | 1974-09-10 | 1980-09-02 | The United States Of America As Represented By The United States Department Of Energy | Reduction of nitrogen oxides with catalytic acid resistant aluminosilicate molecular sieves and ammonia |
US4100421A (en) * | 1975-12-19 | 1978-07-11 | Mitsubishi Denki Kabushiki Kaisha | Ozone-generating apparatus |
US4146372A (en) * | 1976-03-29 | 1979-03-27 | Mittex Aktiengesellschaft | Process and system for recovering water from the atmosphere |
US4367204A (en) * | 1979-05-04 | 1983-01-04 | Budapesti Muszaki Egyetem | Process for the recirculation of nitrogen oxides |
US4336159A (en) * | 1979-09-12 | 1982-06-22 | Ceag Verfahrenstechnik Gmbh | Method and arrangement for the thermal regeneration of charged adsorption materials |
US4398927A (en) * | 1980-07-30 | 1983-08-16 | Exxon Research And Engineering Co. | Cyclic adsorption process |
US4631074A (en) * | 1981-12-15 | 1986-12-23 | Didier-Werke Ag | Method and apparatus for reducing the temperature of air |
US4473381A (en) * | 1982-01-19 | 1984-09-25 | CEAG Verfahrungstechnik GmbH | Method for recovering a substantially dehydrated desorbate as well as apparatus for carrying out the method |
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US9408994B2 (en) | 2008-09-22 | 2016-08-09 | Geno Llc | Conversion of nitrogen dioxide (NO2) to nitric oxide (NO) |
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Also Published As
Publication number | Publication date |
---|---|
AU458612B2 (en) | 1975-03-06 |
GB1357701A (en) | 1974-06-26 |
CA961239A (en) | 1975-01-21 |
FR2121599A1 (de) | 1972-08-25 |
JPS5123959B1 (de) | 1976-07-20 |
DE2200210A1 (de) | 1972-07-27 |
BE777726A (fr) | 1972-07-05 |
AU3759472A (en) | 1973-07-12 |
DE2200210C3 (de) | 1978-07-13 |
FR2121599B1 (de) | 1974-10-18 |
NL170838C (nl) | 1983-01-03 |
IT948802B (it) | 1973-06-11 |
NL7200138A (de) | 1972-07-10 |
SE382803B (sv) | 1976-02-16 |
NL170838B (nl) | 1982-08-02 |
DE2200210B2 (de) | 1977-11-24 |
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